Manufacture of carbon bisulphide



@y B, M, CARTER MANUFACTURE OF CARBON BISULPHIDE Dec. 27, 193,8.

3 Sheets-Sheet l Filed Oct. 20, 1937 INVENTOR Hernani 4% (brief ATTORNEY B. M. CARTER Dec. 27, 1938.

MANUFACTURE OF CARBONBISULPI-IIDE 5 sheets-sheet 2 Filed OCt. 20, 1937 .ATTORNEY Dec. 27, 1938. B. M. CARTER MANUFACTURE OF CARBON BISULPHIDE Filed Oct. 20, 1957 3 SheetS-Sheeil 5 INVENTOR r www m M m QA .7 y? 5 Patented Dec. 27, 1938 UNITED STATES PATENT OFFICE Bernard M. Carter, Montclair, General Chemical Company,

N. J., assigner to New York, N. Y., a

`corporation of New York Application October 20, 1937, Serial No. 169,985

13 Claims.

This invention relates tothe manufacture of carbon ybisulphide by combining sulphur and carbon. More particularly the invention 1is directed to improvements in productionof carbon bisulphide -in processes in which the yCS2 forming 4reaction is carried out lin the presence of appreciable amounts of oxygen, -for example where sulphur dioxide gas-is used as a source of sulphur.

Production of carbon bisulphide from sulphur `dioxide gas and solidecarbonaceous material such las "Wood charcoal has been suggested. In most Vprevious'methods, however, the carbon bisulphide vyield has been low, of the order of 35%, the remaining sulphur having been lost as COS and unreacted elemental sulphur. In the present specification the term yield is used to define kthe percentage of sulphur, introduced into the kreaction,.e. g. as sulphur dioxide, which is converted to carbon bisulphide. -Acid sludges, constituting Waste products of oil rening processes -in which sulphuric acid lis used, may be decomposedbyheating -to produce sulphur dioxide gas and solid carbonaceous vcoke-like residues. Acid sludge coke containing little-or no volatile matter is a particularly active'type ofvcarbonaceous material and may be used as asource of carbon in vthe manufacture of carbon bisulphide. Commerfcially, carbon bisulphide has been commonly produced by reacting sulphuxgusually in the form of sulphurvapor, and WoodcharcoaL'at high temperatures, e. g. around :1450-1650 F. in externally .heated pots or retorts. ySuch retorts are pearshaped and small, being generally. not more than .about BOinchesfn diameter.l Ithas been impractical to make the retortsany ,larger because the high external temperatures required to `force the necessary heat `to thecenter ofthe .reaction Ymass would be prohibitive. The retorts have been made of cast iron and are relatively short-lived on account. of thedeterioratingeiects of the high temperatures externally applied and the corrosive effects of sulphur and of the carbon bisulphide produced. Furthermore, large numbers of such retorts are required to obtain any substantial production of product. and maintenance costs are high, retort replace- `ments `constituting a major'portion of operating costs.

In processes for the manufacture of carbon bisulphide Where the CS2 forming reaction is carried out in the presence of oxygen, for example Where oxygen is vintroduced into the CS2 reaction zone as the oxygen of SO2,l variable but substan- :tial amounts of C'OS are formed. Such COS formationcuts down the CS2y yield and causes loss of Consequently, installation sulphur as COS. The principal object of the present invention is to provide for the manufacture of carbon bisulphide, in procedures ofthe type mentioned where oxygen is present in the CS2 formation reaction, by a method by which there may be obtained carbon bisulphide yields as high asy 75-80%. The invention also aims to provide methods by which loss of sulphur as COS is eliminated or substantially reduced, and lby which the necessity for Yproducing elemental sulphur or SO2 from COS tail gases and making provision for disposal of obnoxious Waste gases are avoided. Another object of the l invention is to provide a'method in which sulphur dioxide gases and acid sludge cokes, both de rived from waste material such as .acid sludges, may be used in place of brimstone and Wood charcoal, the previously utilized more expensive materials. A further object of the invention is to overcome the disadvantages mentioned above in connection with the apparatus `usually employed in the manufacture of carbon bisulphide. The invention affords processes in Which a different rtype of apparatus, cheaply built and maintained, may be employed. To this endthe .invention provides processes by means of which the reaction zone may be heated internally, that is, heat needed to maintain the endothermic reaction is supplied directly to the interior of or generated Within the reaction Zone.

The yinvention is directed to methods for increasing the overall CS2 yields Where the CS2 formation reaction is carried Vout in a reaction Zone containing oxygen the presence of Which seems to invariably tend to increase COS formation. Hence, the principles of the invention are 4applicable in .any situation Where the reactants introduced into the reaction zone contain oxygen, Whether as oxygen of SO2 or COS, as oxygen of CO or CO2 which possibly might be introduced vinto the reaction zone along with sulphur vapor, or oxygen in other form depending upon the source and nature of the sulphur fed into the reaction zone to supply the sulphur needed to combine with the carbon. However, the principles of the invention may be employed to substantial commercial advantage When using sulphur dioxide gas as a source of sulphur, and accordingly the invention will be described in this connection.

In carrying out a preferred embodiment of the invention, when starting operations, sulphur dioxide for example, is introduced into a reaction zone containing a sufficiently active form of carbon and maintained at temperatures high enough to'eect combination of sulphur and carbon to produce carbon bisulphide. The exit gas Ymixture ofthe reaction zone comprises CS2, VCOS and e inerts chiefly CO and CO2. The CS2 and the COS The COS gas is then contacted with carbon;V

preferably by mixing the COS with the fresh SO2 entering the system, the resulting SO2-COS gas mixture being passed through the reaction Zone. As before, the CS2 and theY COS formed are separated from the other reactionproducts, CS2 and COS separated from each other, the CS2 being recovered as product and the COS again re` turned to the reaction zone mixed with incoming SO2. The process of the invention when under way and operated in a continuous manner is a cyclic procedure'in which substantially all of the C'OS formed in the operation is recycled continuouslythrough the reaction zone. Y ,Y Y

The nature of the invention, the details, objects and advantages thereof may be more fully understood from a consideration of the following description taken `in connection with the accom-V panying drawings, in which Figs. 1 and 2 constitute aA diagrammatic illustration of a plant lay-out; Y Fig. 3 is a vertical section of an individual reaction chamber; and Y Fig. lis a diagrammatic illustration of a modied plant lay-out. 1

As indicated, concentrated sulphur dioxidegas Y and the carbonaceous material used in theimproved .process as sources of sulphur and carbon are preferably sulphur dioxidegases and acidv sludge coke. obtained by decomposition of sulphuric acid sludges constituting waste products of oil refining processes.V YReferring. particularly to the sulphurrdioxide and acid sludge coke'production unit of the plant layfout of Fig. l of the drawings, l indicates an acid sludge decomposing retort. The particular construction of the retort is no part of the invention although the sludge is preferably decomposed in Vthe absence of air or other diluting gases by external heating.. Re-l tort l!) may consist for exampleof a xed drum Vor chamber extending through furnace setting I lY and may be equipped with rabbles or a screw conveyor by which the coke formed during decomposition of the sludge is continuously discharged from retort l0 through an outlet' I2 and collected in a coke storage chamber i3. A rotary kiln may be employedif desired. Acid sludgevmay be fed into the retort from tank I4 through pipeV l5 lcontaining a suitable control valve.

YOne end of gas conduit i6 opens into the interior of the sludge decomposingchamber and aords means for conducting the gases and vapors generated by decomposition of the sludge into the bottom of a 'cooling tower Il. The latter .may be a vertical cylindrical vessel provided at the top with a spray arranged to create in the tower a downwardly flowing spray of water or other coolingliquid introduced throughpipe I8. Water and `oil condensate run out of the bottom of the tower through an outlet pipe into a receiving tank 20. After rising through the tower, countercurrent to the cooling liquid,the cooled sulphur dioxide gases are discharged from the top of the tower into gas line 2| connected to drying tower 22.

Fig. 1 shows reaction chambers 25 and 26 dia-v grammatically. As illustrated in Fig. 3, reaction chamber 25 comprises a verticallyelongated steel shell 28 provided with a lining 29 of suitable resistant refractory material such as rebrick. In the lower end of the reaction chamber is a perforated arch 3U aording support forV a bed 3l of charcoal or coke of substantial depth. Solid carbonaceous material, -asrfrom coke bin I3, is fed into the top of the reaction chamber from hopper 35 by an air-lock v35. Air for use during the blasting cycle `is charged into the top of the reaction chamber through pipe lfprovided with a control valve 38. The hot gases'produ'ced during the blasting cycle are discharged from the bottom of the reaction 'chamber through pipe 40 controlled by valve AI. Sulphur dioxide gas is introduced Vinto the top of the reaction chamber through conduit 43 having a Vcontrol valve M, and carbon bisulphide, other gases and vapors formed during the reaction ilow through pipe 45, having a con-- trol valve 47, into outlet header 49. Reaction chamber 26 is built the same as chamber 25 of Fig. 3. As shown in Fig. 1, air inlet pipe 31 of Y chamber'25 is connected to'an air inlet header 5| which communicates with air inlet pipe 52 of' Combustion'gas outlet pipe 4Q of chamber 25 and combustion gas outlet pipe 58 of chamber 26 feed into a connection S0 which may be used to conduct the hot combustion gases to the plant stack or to boilers or heat exchangers in the system. Y

In carryingV out the-process of the invention, relatively concentrated sulphur dioxide gas produced in any Way, and any form of active carbon such as wood charcoal may be used as sources of sulphur andA carbon, although it is preferred to use concentrated sulphur dioxide gases and acid vsludge coke which may be produced in the sludge Y decomposing unit shown in Fig. 1 as follows:

Acid sludges, resulting from refining of hydrocarbon oils with sulphuric acid, vary widely in composition. One representative sludge was found tro'have a titratable acidity of about 50.8% expressed as I-I2SO4, and yieldedon decomposition by destructive distillation about 28% vresidual coke, and a retort gas which, after cooling to 'about normal temperatures, produced about 6% oils'to produce sulphur dioxide gas and sludgeY coke,.decomposition of the sludge is preferably effected by externally heating a body of sludge,

uin a substantially air-tight, elongated kiln or retort, mounted in a furnace setting and arranged to provide Yforfeed of sludge into and withdrawal of sulphur dioxide gases from one end, discharge of residual coke fromV the other end, and maintenance of the higher temperatures at the coke discharge end and lower Vtemperatures at the sludge inlet end. The burners in the furnace combustion chamber H are controlled so as to maintain sludge material temperatures in the retort not less than about 300 F. at the cold end and not more than about 700 F. at theY hot end. It is preferred to maintain temperatures of about 325 F. at sludge inlet end and about 450 F. at 75 is reduced by hydrocarbons and/or by the carbonaceous matterpresent in the sludge, and the gas mixture evolved contains sulphur dioxide and water'vapor, as themajor constituents, together with smaller Vquantities of hydrocarbon vapors,

carbon dioxide, carbon monoxide and nitrogen.

Preferably, decomposition of the sludge is effected at temperatures such as above noted, and underv such conditions that decomposition' proceeds only to Vapproximately a point at which most of the free and/or combined sulphuric acid initiallycontainedin the sludge is reduced, In this situation, the solid carbonacecus residues formed usually contain appreciable quantities of volatile hydrocarbons. In the case of some sludges the Volatile matter content of this residue may run in excess of IEB-40%. Sludge coke produced by the above method and discharged from retort lli into coke storage bin i3 may analyze substantially as follows:

- Percent Total acidity I-I2S04 2.1 4Ash 1.2 Totalvolatilematter, including H2SO4 32.1 Fixed carbon 66.7

The gases formed in retort Il) by decomposition of the sludge and discharged into pipe connection I5 contain generally not substantiallyy in excess of by volume of sulphur dioxide, around 'l5-80% water vapor, and smaller quantities of hydrocarbon vapors and carbon dioxide. The retort gas flows through line I6 into cooling tower l1 and is contacted therein with a downwardly flowing stream of water introduced through pipe i8. The gas stream rising through the tower is cooled, and the bulk of the water Where the gas contains diluents the saine may comprise small quantities of CO2, CO, N2 and hydrocarbons. Although it is preferred to use strong sulphur dioxide gases of the type mentioned, weaker gases may be employed if desired. For example', sludge may be decomposed in retort I0 by direct contact with ho-t combustion gases in which case, on account of dilution of the retort gas, the concentration ofthe gas in line 2| may be as lo-w as 25% sulphur dioxide. Whatever the source of the sulphur dioxide gases, the sulphur dioxide concentration preferably is not substantially less than about by volume, it having been found that where the gas is more dilute, relatively tool much heat is required to heat up the large volume of inert gas to the reaction temperature of sulphur dioxide and carbon.

It is preferable to use in the reaction chambers 25 and 23 sludge material coke, such as that indicated above from which the volatile matter has been expelled by heating to temperatures of around 1400l650 F. for a suiiicient period of time, e. g. 2-6 hours to drive preferably substantially all the volatile matter out of the coke or in any case to reduce the vo-latile matter content of the coketo not more than about 3%. When following this procedure, coke from bin I3 is so treated and then utilized in the reaction chambers 25 and 26. However, when operating in accordance with the preferred embodiments of the invention, the coke recovered in bin i3, for example, a coke such as mentioned above containing substantial quantities of volatile matter, may be charged directly into a reaction chamber and the volatile matter may be substantially removed during the air blasting cycle. The volatile matter remaining in the coke after the air blasting contains such a relatively small amount oi hydrogen that'loss of sulphur as I-IzS is of minor importance. It will be appreciated, therefore, that the carbonaceous material charged into reaction chambers 25 and ZS to serve as a sourc'eof carbon may be wood charcoal, coke as recovered in receptacle i3 containing relativelyl large amounts of rvolatile matter, or such coke from which the volatile matter has been previousiy substantiallyr all removed. A supply of whatevertype oi carbonaceous material to be used is' maintained in hoppers 34 on top of the reaction chambers.

Carbonaceous material of whatever suitablekind used, preferably the acid sludge coke co-ntaining substantial amounts of volatile matter, is fed from hopper 3d into the reaction chamber 25. When starting up operations, valves 44 and 4'! in lines 43 and 46 are closed. Following initial ignition of the coke, air is. fed into the top oi the chamber from pipe 3l and air blowing is continued until the temperature of the reaction chamber 25 and of the material therein is at least aboutv 200 or 300 F. in excess of about 1450-1475o F. To secure the most economical operating results, however, it is desirable to continue the air blasting cycle until the temperature in the reaction` chamber is raised to at least about 2000 F., and preferably inthe neighborhood of 2000230 F. When using sludge coke containing substantial amounts of volatile matter, blasting should be continued long enough and the temperature raised high enough to reduce the volatile matter content (i. e., chiefly hydrocarbons) of the coke to not more than about 3%. Where air blasting is carried out until the temperature of the reaction chamber is about 2000 F., such temperatures are suiciently high to insure reduction of the volatile matter content tothe desired degree. It will be understood, however, it is not necessary to raisethe temperature of the reaction chamber to 2000 since the volatile matter content of the coke may be reduced b-y blasting at lower temperatures for relatively longer periods of time.

When air is blown through the hot coke bed, carbon is burned iirst vto CO2 which tol a considerable extent is reduced to CO by further contact with hot coke. The hot blasting cycle exit gases comprising chiey nitrogen, carbon dioxide and carbon monoxide pass out of chamber 25 by pipe lli! and flow into connection 69 from whence thev hot waste gases may be drawn for use in boilers or heat exchangers about the plant or for any other purpose desired. It is noted this gasnmay contain substantial amounts of CO which may be burned to generatefurther amounts of heat. After the bed of carbonaceous material in the reaction chamber 25 has been heated as described, Valve 38 in air line 31 and Avalve @l in gas outlet pipe it are closed. Chamber 25 is then-ready and valve 44 in lSO2-COS inlet pipe 43 and valve 47 in carbon bisulphide vapor 'outlet pipe 46 are opened.

The concentrated sulphur dioxide gas in lineV 2i is passed through drying tower 22 where moisactive type of carbon ,to produce a Vgas mixture comprising CS2, COS, and inerts such as CO and CO2; separating CS2 and COS from the other gaseous and/or vaporous reaction products; separating thefCSz from the COS and recovering CS2 as product; further contacting the COS with active carbon, preferably by mixing the COS Vwith the incoming raw SO2 and then passing the resulting SO2-COS gas mixture through the reaction Zone; recovering further CS2 formed as product and again returning the COS to the reaction zone. In other Words, the process of the p invention comprises preferably a cyclic procedure in which substantially al1 of the COS formed in the system is recycled continuouslyV through the reaction zone;

Investigations upon which the invention is 1 based show that for any given set of conditions y the COS content of the exit gases of a CS2 reaction zone is about the same, whether the COS content of the Vreaction gas is or is not recycled through the reaction zone. It thus appears that in the present process, the recycled COS reacts with carbon to produce CS2 and/or acts possibly Y yield may be substantially increased by recycling Y COS produced in a previous cycle of the operation.

The concentrated SO2 gas in line 63 (the exit Y gas of drying tower 22) may contain from 85 to roughly SO2. As will be seen from subsequent disclosure, the COS gas in COS gas line 64 may contain 55-'T0% COS, 5-15% CO, and 1530% inert including possible small amounts of CO2. Gas mixer 65 is provided with orifice meters by means of which quantities of gas fed into the mixer from SO2 line (i3-and from COS line 64 may be regulated. In order to recycle through the reaction chambers 25 or 26 substantially all of the COS formed in the system, under average operating conditions about 25-35% Vof the gas drawn into blower 'ID fromY mixer 65 comprises COS gas from line 64, the balance consisting of concentrated SO2 gas from line 63. Under such conditions the exit gas of mixer 65 may comprise upward of about 65% SO2, the balance consisting of COS plus inert including CO and possibly some CO2. y

The exit gas of mixer 65 is passed into the system by blower 'l0 which forces the gas through line Il and heat exchanger 'l2 into inlet header 42. The gas in line 'H is ordinarily at temperatures of about 100 F. When starting up the process, at which time no hot reaction gases are available for preheating the incoming gas in heat exchanger I2, anysuitable means maybe used to heatV up incoming gases to temperatures of about 800-1000 F. After operations are under way, the incoming gases are heated tovthis extent inV transferrer 12, by heat exchange with Vhot outgoing reaction gases. 'Ihe hot sulphur dioxide gas then flows'from header 42 through pipe 43 into the top of chamber 25.'

Assuming that operations are under way and that a preheated SO2-COS gas mixture, such as mentioned above hasbeen introduced'into the reaction chamber, at the highrtemperatures prevailing in the reaction zone, hot carbon Vand sulphur combine to form CS2 vapors which leave the reaction chamber at temperatures upwards Vof about1500 F. through pipe 46 and enter gas outlet header 49. In one examplawhen employ- K ingi an SO2- COS gas of the nature mentionedv above, the exit gasmixture of the reaction chamber contained substantially no1-12S orrunreacted VSO2rand excluding the CS2 vapor, the gas comprised by volume'about 21% COS,'2.% CO2, 73%

CO, and 4% inert. In this continuous operation,

the CS2 yield, based on the amount of sulphur fed into the system as SO2, was about 77%. In

thisparticular operation, the average temperature in the reaction zone was about 1545 F.

As the reaction taking place in chamber 25 is endothermic, the'temperature inthe reaction zone gradually decreases on Vaccount of loss of heat absorbed by the reaction Vas well as by radiation and heat carried out by Ythe reaction gas. When the temperature in the reaction chamber drops to a point below which further production of carbon bisulphide is not economical, for example 1500 F., valve 44 in SO2 `gas feed pipe 43 and valve 41 in CS2 vapor line 46 are,Y closed and reaction chamber 25 is taken 0E CS2'production. VValve 38 in air line 3T and valve 4| Vin blasting cycle exit gas pipe 4D are opened and air Ais again passed through the reaction chamber to burn sufcientamount of coke to again raise the temperature in the reactionV zone to around 2000-2300 F. From time to time further quantities of coke are added to the reaction chamber 25 from hopper 34. Since coke is fed into the reaction chamber in relatively small increments in the course of operation as described no difficulty is encountered in connection with insuring reduction of the volatile matter content of the coke to the desired extent.

It will be understood that reaction chamber 26 is a duplicate. ofand is arranged in parallel with chamber 25. ,When chamberv 25 is: on the blasting cycle, by suitable regulation of the several valves reaction chamber 2E is operated on the productionrcycle to" form carbon bisulphide. During this phase of operation, it will be understood that valve I5 in SO2 gas supply pipe 1E and V valve H in CSzvapor pipe ,'53 are opened, and

, heat in the reaction zone by burning part of the carbonaceous material used as a source of carbon in the production of carbon bisulphide as described, in instances where it is desired to conserve coke or charcoal, heating up of the reaction zone to the desired temperatures may be advantageously accomplished in other ways. For example, oil, gas or other combustiblematerial in Y suitableV quantities may be injected into the reaction chamber together with the necessary amount of air and burned to raise the temperature of the 75 ping still |01.

reaction zone totherequireddegree. In this instance, although some of the coke orcharcoal in the reaction chamber may be burned, the bulk of the heat needed is supplied by burning of the oil, gas or other fuel and consumption of coke or Ying SO2 gases. The CS2 gases after leaving transferrer 12 are carried by line 9| thru oil preheater 93, (Fig. 2) cooled to about 300 F., and are desirably passed through another cooler in which the gas temperature is reduced to about 100 F.

In accordance with the invention, it has been Yfound that straw oil constitutes a Very suitable material for absorbing both CS2 and COS contained in theY furnace gases. Accordingly, exit gases of cooler 94 are passed into the bottom of a CS2 and COS absorbing tower 08 over which absorbent straw oil is circulated. A supply of vstraw oil is maintained in tank 99 by circulating pump |00. The quantity and rate of ow of oil down thru tower 98 are controlled by valve l0! so as to elect absorption of substantially all of the CS2 and COS contained in the upwardly flowing furnace gases. The proper rateof flow of oil through tower 96 may be readily determined to suit any particular set of operating conditions. In this way substantially all of the COS and CS2 of the gas stream becomes absorbed in the oil and is thus separated from most of the remaining inert furnace gases, principally CO and CO2, which are discharged from the system through line |03.

The eluent oil in tower 98, containing absorbed CS2 and COS, runs through line |05, preheater 93 and line |06, into CS2 and COS strip- This stripper'comprises a tower or column provided with means in the bottom for introduction of live steam and with any suitable reuxing arrangement in the upper part. Oil

rich in'absorbed CS2 and COS is fed into the top of the stripper and steam, at temperature of about 101 C. from boiler 00 and line |09 is introduced into the bottom of the stripper. Stripped oil runs from the'bottom o tower |01 into a suitable separator ||0 in which oil and condensed water are separated, and the separated oil, after cooling to about 100 F. in cooler H2,

' is returned by pump |00 to oil tank 99.

Steam, CS2 vapor and COS gas discharged from the top of stripper |01, iiow through line and through two water-cooled condensers ||6 and ||1 connected in series. These coolers are operated so as to liquefy substantially all of the Water Vand CS2 vapor which together with the COS gas collect in a receiver or separator |20. If desired, condensers ||6 and ||1 may be-refrigerated to eiect maximum condensation of H2O and CS2. In receiverv |20, water and CS2 are separated, the water being discharged to waste and the CS2 run into CS2 storage tank |2|.'

'I'he Lgas discharged from separator |20 into line |22 may comprise 55-'10% COS, 5-15% CO, and 1530% other inert.V Where vthe apparatus units ahead of separator |20 are operating under `optimum conditions, the gas in line: |22 ordinarily contains but little CS2, in which circumstance |29 opened to pass the COS gas from separator |20 directly through lines |22 and |29 into the COS gas header 6d which feeds the COS gas into the mixer 65. However, should operating conditions in apparatusunits preceding separator |20 be such that the COS gas in line |22 contains substantial amounts of CS2, vvalve |28 is closed and'valve |24 opened to conduct CS2-COS gas into the bottom of a second absorbing tower |3|. rPhe `absorber |3l, stripper |32, oil and water separator |33, oil cooler |30, condenser |35, and CS2-COS-H2O receiver and separator |35 are operated in the same way as absorber 98 and stripper |01 and associated apparatus units previously described. Liquid CS2 recovered in separator |36 is. run into CS2 storage tank |2| thru line 20 and the COS exit gas of receiver |36 goes through line MI into COS gas header 64 and thence through valve |26 into mixer 65, the composition ofthe gas in line il being of the nature of that previously mentioned.

Fig. 4 is a diagrammatic illustration of apparatus used in carrying out a modication of the process of the invention. In the apparatus of Fig. 4, acid sludge-SO2 production unit |50, reaction chamber |5l, absorber |52 and stripper |53,

reaction chamber 25, absorber 98, stripper |01,

condensers ||6 and ||1, and CSz-COS-I-IzO separator |20 of Figs. 1 and 2. However, instead of returning the COS exit gas of separator |55 of Fig. 4 to reaction chamber |5| (as in the preferred modification of Figs. 1 and 2) the COS exit gas of separator |55 is run through a line |56 into a second reaction chamber |6|. Absorber |62, stripper |63, condenser |64, and CS2-COS- H2O separator |65 are constructed and operated in the same way as absorber |52, stripper |53, condenser |50, and separator |55 of Fig. 4. However, the COS exit gas of separator |65 is returned through line |66 to and is recycled through reaction chamber |6| which is constructed and Voperated substantially the saine as reaction chambers 25 of Fig. 1 and |5| of Fig. 4, except that in reaction chamber |61 the sulphur-oxygen compound is supplied as COS from line y|56 and recycling line |66.

It has also been found that activated carbon, for example Norite is a satisfactory absorbent for both CS2 and COS, especially for COS. If it is desired to ruse this material, the absorbed CS2 and COS may be released byy heating to say 105 C. If desired, the CS2 may be absorbed in straw oil, and the exit gas of the straw oil absorber passed into an absorber containing activated carbon. The COS subsequently released from the carbon by heating may be fed into the COS gas line 64 to introduce the COS into mixer 65.

While the improved process has been described in connection with use of SO2 gas as the source of sulphur, in which case at least part of the oxygen of the SO2 tends to combine with carbon and sulphur to form COS, it will be understood the vprinciples of the invention are applicable where oxygen is introduced in other forms, for example as COS, CO, or CO2 which gases might be present in the gas mixture entering the reaction zone. To illustrate, the advantages afforded by the invention are available should the sulphur be introduced largely in the form of vapor in a Vgas mixture containing say CO. In

the claims, the expression inert reaction products is intended to include reaction products other than CS2 and COSsuch as CO, CO2, N2, etc. f

I claim:

1. The method for making carbon bisulphide which comprises introducing into a reaction zone containing a body of solid carbonaceous material a stream of sulphurous gas comprising materials of the class consisting of sulphur dioxide, sulphur vapor and carbon oxysulphide maintaining said zone at temperatures suiiiciently high to effect combination of carbon with sulphur of said gas to form carbon bisulphide, withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing said separated carbon oxysulphide and further quantities of said sulphurous gas into said zone to effect formation of further quantities of carbonV bisulp-hide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

2. In the method for making carbon bisulphide involving maintaining a reaction Zone containing carbonaceous material at temperatures sufficiently high to effect combination of sulphur and carbon to produce carbon bisulphide, passing through said zone a stream of sulphurous gas comprising materials of the class Vconsisting of sulphur dioxide, sulphur vapor and carbon oxysulphide, to effect formation of a reaction zone exit. gas mixture containing carbon bisulphide and Vcarbon oxysulphide, separating carbon bisulphide from carbon oxysulphide, and separately recovering carbon bisulphide and carbon oxysulphide; the improvement which comprises Vrecycling the carbon oxysulphide through the reaction zone.

3. In the method for making carbon bisulphide involving maintaining a reaction zone containing solid carbonaceous material at ytemperatures sufficiently high to effect combination of sulphur and carbon to produce carbon bisulphide, passing through said zone a stream of sulphurous gas comprising materials of the class consisting of sulphur dioxide, sulphur Vvapor and carbon oxysulphide, to effect formation of a reaction zone exit gas mixture` containing carbon bisulphide and carbon oxysulphide, and recovering carbon bisulphide from said gasmixture; the improvement which comprises carrying out the reaction in theA presence of carbon oxysulphide formed in a previous reaction.

4. The method for making carbon bisulphide which comprises continuously introducing into a reaction zone containing a body of solid carbonaceous material a stream of sulphurous gas comprising materials of the class consisting of sulphur dioxide, sulphur vapor and carbon oxysulphide, maintaining said zone at temperatures suciently high to effect combination of carbon with sulphur of. said gas to form carbon bisulphide, continuously withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, continuouslyV separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, and continuously returning said separated carbon oxysulphide to said zone. Y

5. The method for making carbon bisulphide which comprises introducing into a reaction zone containinga body of solid carbonaceous material a-stream of sulphurdioxide gas, maintainring said zone at temperatures `sufficiently high to effect combination -of carbon and sulphur of said sulphur dioxide gas, to form carbon bisulphide, withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing Vsaid separated carbon oxysulphide and further quantities of sulphur dioxide into said zone to eiect formation of further Vquantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

6. The method for making carbon bisulphide which comprises introducing into a reaction zone containing a body of solid carbonaceous material an incoming stream of gas-containing carbon oxysulphide gas, maintaining said zone at temperatures su'iciently high to effect combination of carbon of said solid carbonaceous material with sulphur of said carbon oxysulphide gas to form carbon bisulphide, withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing said separated carbon oxysulphide and further quantities of said incoming carbon oxysulphide gas into said zone to eiect formation of further quantities of carbon bisulphide, and recovering' further quantities of carbon bisulphide from the reaction zone exit gas mixture.

7. The method of making carbon bisulphide which comprises introducing into'a reaction zone containing a body of solid carbonaceous material a stream of sulphurous gas comprising materials of the class consisting of sulphur dioxide, sulphur Vapor and carbon oxysulphide, maintaining said Zone at temperatures sufficiently high to effect combination of carbon with sulphur of said gas to form carbon bisulphide, withdrawing from the reaction Zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, contacting said gas mixture with an absorbent adapted to absorb both carbonbisulphide and carbon voxysulphide to separate carbon bisulphide and carbon oxysulphide from inert reaction products, separating carbon bisulphide and carbon oxysulphide from the absorbent and separately recovering carbon bisulphide and carbon oxysulphide, introducing said carbon oxysulphide and further quantities of said sulphurous gas into said zone to effect formation of further quantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

8. The method forY making carbon bisulphide which comprises introducing into a reaction Zone containing a body of solid carbonaceous material a stream of sulphur dioxide gas, maintaining said zone at temperatures suiciently high to eiect combination of carbon with sulphur of said sulphur dioxide to form carbon bisulphide, withdrawing from the reaction Vzone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, contacting said gas mixture with straw oil under conditions to eiect separation of both carbon bisulphide Vand carbon oxysulphide from inert reaction products, separating carbon bisulphide and carbon oxysulphidefrom the straw oil by steam distillation,

cooling the resultant gas-Vapor mixture to condense carbon bisulphide and separate the same from the carbon oxysulphide, recovering carbon bisulphide, introducing said separated carbon oxysulphide and further quantities of sulphur dioxide into said zone to eiect formation of further quantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

9. The method for making carbon bisulphide which comprises introducing into a reaction zone containing a body of solid carbonaceous material a stream of sulphurous gas comprising materials of the classconsisting of sulphur dioxide, sulphur Vapor and carbon oxysulphide, maintaining said zone at temperatures suiiiciently high to effect combination of carbon with sulphur of said gas to form carbon bisulphide, withdrawing from the reaction Zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing said Separated carbon oxysulphide and a greater proportion by volume of further quantities of said sulphurous gas into said Zone to effect formation of further quantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

10. The method for making carbon bisulphide which comprises introducing into a reaction zone containing a body of solid carbonaceous material a stream of sulphur dioxide gas, maintaining said zone at temperatures sufliciently high to eiect combination of carbon with sulphur of said sulphur dioxide gas to form carbon bisulphide, withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing said separated carbon oxysulphide into contact with a body of solid carbonaceous material at temperatures suiciently high to eiect combination of carbon of such solid carbonaceous material with sulphur of said separated carbon oxysulphide to eiect formation of further quantities of carbon bisulphide.

11. The method for making carbon bisulphide which comprises introducing into a reaction zone containing a body of solid carbonaceous material a stream of sulphurrdioxide gas, maintaining said zone at temperatures sumciently high to effect combination of carbon with sulphur of said sulphur dioxide gas to form carbon bisulphide, withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing said separated carbon oxysulphide into a second reaction zone containing a body of solid carbonaceous material, maintaining said second zone at temperatures sufciently high to effect combination of lcarbon of such solid carbonaceous material with sulphur of said separated carbon oxysulphide to effect formation of further quantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the exit gas mixture of said second zone.

12. The method for making carbon bisulphide which comprisesl decomposing sludge material, derived from sulphuric acid treatment of petroleum oils, by heating to form solid carbonaceous residue and hot sulphur dioxide gas mixture containing 'condensable vapors, cooling the hot gas mixture to condense the bulk of the condensable vapors and form a concentrated sulphur dioxide gas, introducing a stream of the sulphur dioxide gas into a reaction Zone containing a body of solid carbonaceous material, maintaining said zone at temperatures sufficiently high to eiect combination of carbon with sulphur of said sulphur dioxide gas to form carbon bisulphide, withdrawing from the reaction Zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products', separating the carbon bisulphide and carbon oxysulphide from inert reaction products, recovering carbon bisulphide, introducing said separated carbon oxysulphide and further quantities of said concentrated gas into said zone to effect formation of further quantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

13. The method for making carbon bisulphide which comprises decomposing sludge material, derived from sulphuric acid treatment of petroleum oils, by heating to form solid carbonaceous residue and hot sulphur dioxide gas mixture containing condensable vapors, cooling the hot gas mixture to condense the bulk of the condensable vapors and form a concentrated sulphur dioxide gas, introducing a stream of the sulphur dioxide gas into a reaction Zone containing a body of said solid carbonaceous residue containing not more than about 3% Volatile matter, maintaining said zone at temperatures sufciently high to eiect combination of carbon With sulphur of said sulphur dioxide gas to form carbon bisulphide, withdrawing from the reaction zone an exit gas mixture containing carbon bisulphide, carbon oxysulphide and inert reaction products, contacting said gas mixture with straw oil under conditions to effect separation of both carbon bisulphide and carbon oxysulphide from inert reaction prcducts, separating carbon bisulphide and carbon oxysulphide from the straw oil by steam distillation, cooling the resultant gas-vapor mixture to condense carbon bisulphide and separate the same from the carbon oxysulphide, recovering carbon bisulphide, introducing said separated carbon oxysulphide and a greater proportion by volume of further quantities of said concentrated sulphur dioxide gas into said zone to effect ormation of further quantities of carbon bisulphide, and recovering further quantities of carbon bisulphide from the reaction zone exit gas mixture.

BERNARD M. CARTER. 

